CN210220390U - Three-cycle natural gas liquefaction device suitable for ultra-large scale - Google Patents
Three-cycle natural gas liquefaction device suitable for ultra-large scale Download PDFInfo
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- CN210220390U CN210220390U CN201920872645.2U CN201920872645U CN210220390U CN 210220390 U CN210220390 U CN 210220390U CN 201920872645 U CN201920872645 U CN 201920872645U CN 210220390 U CN210220390 U CN 210220390U
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- propane
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- wmr
- natural gas
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 118
- 239000003345 natural gas Substances 0.000 title claims abstract description 52
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims abstract description 260
- 239000001294 propane Substances 0.000 claims abstract description 130
- 239000003507 refrigerant Substances 0.000 claims abstract description 37
- 238000005057 refrigeration Methods 0.000 claims abstract description 35
- 230000004087 circulation Effects 0.000 claims abstract description 16
- 239000007788 liquid Substances 0.000 claims description 31
- 238000000926 separation method Methods 0.000 claims description 28
- 238000004781 supercooling Methods 0.000 claims description 13
- 238000001816 cooling Methods 0.000 claims description 11
- 239000007789 gas Substances 0.000 claims description 5
- 238000000034 method Methods 0.000 abstract description 29
- 239000002994 raw material Substances 0.000 abstract description 3
- 230000008092 positive effect Effects 0.000 abstract description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 10
- 239000007791 liquid phase Substances 0.000 description 10
- 238000005516 engineering process Methods 0.000 description 8
- 239000012071 phase Substances 0.000 description 7
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 6
- 238000010276 construction Methods 0.000 description 6
- 238000005265 energy consumption Methods 0.000 description 5
- 229910052757 nitrogen Inorganic materials 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- 239000005977 Ethylene Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 2
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 2
- 238000007906 compression Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/0042—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by liquid expansion with extraction of work
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
- F25J1/0057—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream after expansion of the liquid refrigerant stream with extraction of work
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/008—Hydrocarbons
- F25J1/0087—Propane; Propylene
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
- F25J1/0217—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as at least a three level refrigeration cascade with at least one MCR cycle
- F25J1/0218—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as at least a three level refrigeration cascade with at least one MCR cycle with one or more SCR cycles, e.g. with a C3 pre-cooling cycle
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
- F25J1/0262—Details of the cold heat exchange system
- F25J1/0263—Details of the cold heat exchange system using different types of heat exchangers
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0281—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc. characterised by the type of prime driver, e.g. hot gas expander
- F25J1/0283—Gas turbine as the prime mechanical driver
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant gas
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The utility model discloses a three circulation natural gas liquefaction device suitable for super large-scale, the device includes natural gas liquefaction pipeline, propane precooling circulation system, WMR refrigeration cycle system and CMR refrigeration cycle system. Compared with the prior art, the utility model has the positive effects that: the utility model discloses based on three circulations, share every grade of refrigeration load, the natural gas loops through 1 finned plate heat exchanger and 2 around tubular heat exchangers and cools off, until liquefaction subcooling, and process equipment is small in quantity, and natural gas liquefaction device scale can reach single 600 ~ 800 ten thousand tons/year; the cold energy required by the liquefaction process is provided by three systems of propane, WMR mixed refrigerant and CMR mixed refrigerant, the system has rich adjusting means, can provide matched cold energy for the natural gas liquefaction process, and has flexible operation and good adaptability to raw materials.
Description
Technical Field
The utility model relates to a cryogenic technical field of natural gas liquefaction specifically is a three circulation natural gas liquefaction device suitable for super large-scale, through adopting tertiary refrigeration cycle, the load of distribution precooling section, liquefaction section and supercooling section adopts high efficiency equipment, simplifies the flow, satisfies single-row productivity 600 ~ 800 ten thousand tons/year super large-scale natural gas liquefaction device construction demand.
Background
With the continuous development of LNG technical equipment, the general trend of international LNG plant construction is towards large-scale development, the single-row production capacity is more 300-550 ten thousand tons/year in scale, and the maximum scale reaches 780 ten thousand tons/year. The liquefaction process technologies adopted for the international large-scale LNG plant construction mainly comprise C3MR, DMR and AP-X processes of APCI company, Optimized Cascade process of Conphyra company, MFC process of Linde company and DMR process of Shell company. The large-scale LNG device can reduce unit LNG production cost and realize scale benefits.
The single-row maximum scale of the domestic LNG device is 120 ten thousand tons/year, and a multi-stage single-component refrigeration liquefaction process (MSC process) is adopted. The development of a single-row 350-ten-thousand-ton/year natural gas liquefaction process package is realized based on the MSC process, but the process cannot meet the single-row 600-800-ten-thousand-ton/year ultra-large-scale LNG device construction.
Therefore, it is necessary to develop a natural gas liquefaction process which can be applied to a 600-800 ten thousand tons/year ultra-large scale natural gas liquefaction device.
Disclosure of Invention
In order to overcome the shortcoming of the prior art, the utility model provides a be applicable to super large-scale three circulation natural gas liquefaction device has the advantage that the flow is succinct, the energy consumption is low.
The utility model adopts the technical proposal that: the utility model provides a three circulation natural gas liquefaction devices suitable for super large-scale, includes natural gas liquefaction pipeline, propane precooling circulation system, WMR refrigeration cycle system and CMR refrigeration cycle system, wherein:
the natural gas liquefaction pipeline is formed by sequentially connecting a propane heat exchanger, a WMR heat exchanger, a CMR heat exchanger, an LNG expander, an LNG flash tank and an LNG booster pump;
the propane precooling circulating system comprises a propane heat exchanger, a propane compressor outlet cooler, a high-pressure propane gas-liquid separation tank, a medium-pressure propane gas-liquid separation tank and a low-pressure propane gas-liquid separation tank, and is used for precooling natural gas, WMR refrigerant and CMR refrigerant;
the WMR refrigeration cycle system comprises a WMR heat exchanger, a WMR compressor inlet buffer tank, a WMR compressor outlet cooler and a WMR expander and is used for further cooling and partially liquefying natural gas and CMR refrigerant;
the CMR refrigeration cycle system comprises a CMR heat exchanger, a CMR compressor inlet buffer tank, a CMR compressor outlet cooler and a CMR expander and is used for providing refrigeration capacity for the complete liquefaction and supercooling of natural gas and CMR refrigerant.
Compared with the prior art, the utility model has the positive effects that:
the utility model discloses based on three circulations, share every grade of refrigeration load, the natural gas cools off through 1 finned plate heat exchanger and 2 coiled tube heat exchangers in proper order, until the liquefaction subcooling, and process equipment is small in quantity, and natural gas liquefaction device scale can reach single 600 ~ 800 ten thousand tons/year; the cold energy required by the liquefaction process is provided by three systems of propane, WMR mixed refrigerant and CMR mixed refrigerant, the system has rich adjusting means, can provide matched cold energy for the natural gas liquefaction process, and has flexible operation and good adaptability to raw materials. Compared with the prior art, the method has the following characteristics:
1. the utility model discloses an innovation and improvement that go on the basis of multistage monocomponent liquefaction technology (MSC technology) engineering application practice, technology has the continuity, compares with MSC technology, has following advantage:
1) in the MSC process, propylene precooling, ethylene cooling and mixed refrigerant liquefaction supercooling (the mixed refrigerant mainly comprises methane and nitrogen) are adopted. In the utility model, the precooling circulation adopts propane, the cooling circulation adopts mixed refrigerant, mainly ethane, including methane and propane; the liquefied supercooling circulating refrigerant adopts a mixed refrigerant comprising nitrogen, methane and ethane.
2) The cooling section and the liquefaction supercooling section both adopt mixed refrigerants, can be combined with a drive device to select machine types to adjust various refrigeration cycle loads, flexibly adjusts the cooling, liquefaction and supercooling temperatures of the natural gas, and has better operation adaptability.
3) In the MSC process, a shell-and-tube heat exchanger or a CIK heat exchanger is adopted for a propylene and ethylene refrigeration system to exchange heat, and a plate-fin heat exchanger is adopted for methane refrigeration circulation; the propane precooling section heat exchange equipment adopts the efficient plate-fin heat exchanger, the integration level of a heat exchange system is high, and the propane precooling section heat exchange equipment has the advantages of simplified process flow, less occupied land and the like; the utility model discloses well WMR and CMR main cryogenic heat exchanger adopt the tubular heat exchanger, and the tubular heat exchanger has the big characteristics of single heat transfer area, is favorable to realizing that the natural gas liquefaction device is upsized.
2. Two mixed cryogen liquefaction technology (DMR technology) adopt 2 grades of mixed cryogen refrigeration cycle to realize natural gas precooling, liquefaction and subcooling, compare with the DMR technology, the utility model discloses a three circulation refrigeration share liquefaction loads at different levels, realize single 600 ~ 800 ten thousand tons/year super large-scale natural gas liquefaction device construction.
3. The MFC process is a three-cycle refrigeration cycle process, and a pre-cooling section, a liquefying section and a supercooling section of the MFC process are all refrigerated by adopting a mixed refrigerant; compared with MFC, the utility model discloses precooling section is pure propane cryogen.
4. AP-X is also a three-cycle refrigeration cycle process, wherein a propane refrigeration section is adopted in a precooling section, a mixed refrigerant refrigeration section is adopted in a liquefying section, and a nitrogen expansion refrigeration section is adopted in a supercooling section; compared with the AP-X process, the utility model discloses mixed cryogen refrigeration is adopted to the super-cooled section.
5. The utility model discloses WMR throttle, CMR throttle and high-pressure LNG throttle all adopt liquid turboexpander, and liquid turboexpander is the isentropic expansion, compares with the isenthalpic expansion of conventional choke valve, and expansion efficiency is high, and LNG product output can improve 1 ~ 3%, and unit LNG product energy consumption reduces 1 ~ 3%.
Drawings
The invention will now be described, by way of example, with reference to the accompanying drawings, in which:
fig. 1 is a process flow diagram of the present invention.
Detailed Description
A three cycle natural gas liquefaction plant suitable for ultra large scale, as shown in figure 1, comprising: propane precooling plate-fin heat exchanger 1, WMR coiled-tube heat exchanger 2, CMR coiled-tube heat exchanger 3, LNG hydraulic turboexpander 4, LNG flash tank 5, LNG booster pump 6, propane compressor 7, propane compressor outlet cooler 8, first high-pressure propane throttle valve 9, second high-pressure propane throttle valve 10, high-pressure propane gas-liquid separation tank 11, first intermediate-pressure propane throttle valve 12, second intermediate-pressure propane throttle valve 13, intermediate-pressure propane gas-liquid separation tank 14, low-pressure propane throttle valve 15, low-pressure propane gas-liquid separation tank 16, WMR compressor inlet buffer tank 17, WMR compressor 18, WMR compressor outlet cooler 19, WMR hydraulic turboexpander 20, CMR compressor inlet buffer tank 21, CMR compressor 22, CMR compressor outlet cooler 23, CMR hydraulic turboexpander 24, wherein:
the propane precooling plate-fin heat exchanger 1, the WMR wound-tube heat exchanger 2, the CMR wound-tube heat exchanger 3, the LNG hydraulic turboexpander 4, the LNG flash tank 5 and the LNG booster pump 6 are sequentially connected.
The propane compressor 7, the propane compressor outlet cooler 8, the first high-pressure propane throttle valve 9, the propane precooling plate-fin heat exchanger 1 and the high-pressure suction inlet of the propane compressor 7 are sequentially connected;
an outlet cooler 8 of the propane compressor, a second high-pressure propane throttling valve 10, a high-pressure propane gas-liquid separation tank 11, a first medium-pressure propane throttling valve 12, the propane precooling plate-fin heat exchanger 1 and a medium-pressure suction inlet of the propane compressor 7 are sequentially connected;
the high-pressure propane gas-liquid separation tank 11, the second medium-pressure propane throttle valve 13, the medium-pressure propane gas-liquid separation tank 14, the low-pressure propane throttle valve 15, the propane precooling plate-fin heat exchanger 1, the low-pressure propane gas-liquid separation tank 16 and the low-pressure suction inlet of the propane compressor 7 are sequentially connected;
the gas phase at the outlet of the high-pressure propane gas-liquid separation tank 11 is connected with a high-pressure suction pipeline of a propane compressor 7; the gas phase outlet of the medium-pressure propane gas-liquid separation tank 14 is connected with a medium-pressure suction pipeline of the propane compressor 7.
The WMR compressor inlet surge tank 17, the WMR compressor 18, the WMR compressor outlet cooler 19, the propane precooled plate-fin heat exchanger 1, the WMR coiled-tube heat exchanger 2, and the WMR hydraulic turboexpander 20 are connected in series.
The CMR compressor inlet buffer tank 21, the CMR compressor 22, the CMR compressor outlet cooler 23, the propane precooling plate-fin heat exchanger 1, the WMR wound-tube heat exchanger 2, the CMR wound-tube heat exchanger 3 and the CMR hydraulic turboexpander 24 are connected in sequence.
The utility model discloses when carrying out the natural gas liquefaction, including following content:
1) the propane precooling system precools the natural gas, the WMR and the CMR to the temperature of-30 ℃ to-39 ℃:
the propane pressurized to 1.5 MPa.a-2.5 MPa.a from a propane compressor 7 is cooled to 20-50 ℃ by a propane cooler 8 and divided into 2 strands, wherein one strand of liquid-phase propane (about 15-25%) is throttled by a first high-pressure propane throttle valve 9, enters a propane precooling plate-fin heat exchanger 1 after the pressure is reduced to 0.3 MPa.a-0.6 MPa, cools natural gas, WMR refrigerant and CMR refrigerant (20-0 ℃) and returns the gas-phase propane coming out of the plate-fin heat exchanger 1 to a high-pressure suction inlet of the propane compressor 7; the other liquid-phase propane (75-85%) is throttled by a second high-pressure propane throttle valve 10, the pressure is reduced to 0.3 MPa.a-0.6 MPa.a, the liquid-phase propane enters a high-pressure propane gas-liquid separation tank 11 for gas-liquid separation, and gas-phase propane at the top of the tank returns to a high-pressure suction inlet of a propane compressor 7;
the liquid phase of the high-pressure propane gas-liquid separation tank 11 is divided into 2 strands, wherein one strand of liquid-phase propane (45-55%) is throttled by a first medium-pressure propane throttle valve 12, the pressure is reduced to 0.2 MPa.a-0.35 MPa.a, the liquid-phase propane enters a propane precooling plate-fin heat exchanger 1, natural gas, WMR refrigerant and CMR refrigerant are cooled to (-10 ℃ -minus 20 ℃), and gas-phase propane coming out of the plate-fin heat exchanger returns to a medium-pressure suction inlet of a propane compressor 7; the other liquid-phase propane (45-55%) is throttled by a second medium-pressure propane throttling valve 13, the pressure is reduced to 0.2 MPa.a-0.35 MPa.a, then the liquid-phase propane enters a medium-pressure propane gas-liquid separation tank 14 for gas-liquid separation, and the gas-phase propane on the top of the tank returns to a medium-pressure suction inlet of a propane compressor 7;
the liquid phase of the medium-pressure propane gas-liquid separation tank 14 is throttled by a throttle valve 15, the pressure is reduced to 0.1 MPa.a-0.2 MPa.a, the liquid phase enters a propane precooling plate-fin heat exchanger 1, natural gas, WMR refrigerant and CMR refrigerant are cooled to (-30 ℃ to-39 ℃), and gas-phase propane discharged from the propane precooling plate-fin heat exchanger 1 passes through a low-pressure propane gas-liquid separation tank 16 and then returns to a low-pressure suction inlet of a propane compressor 7;
the low-pressure propane, the medium-pressure propane and the high-pressure propane are pressurized by a propane compressor 7 and then circulated.
2) The WMR refrigeration system cools the natural gas and the CMR refrigerant to-65 ℃ to-95 ℃:
WMR refrigerant coming out from the bottom of the WMR coiled tube heat exchanger 2 enters a WMR compressor inlet buffer tank 17, is pressurized to 3 MPa.a-5 MPa.a by a WMR compressor 18, is cooled to 20-50 ℃ by a WMR cooler 19, enters a propane precooling plate-fin heat exchanger 1, is cooled to-30-39 ℃ and is liquefied; the liquid WMR enters the WMR coiled pipe type heat exchanger 2 to be further cooled to the temperature of minus 65 ℃ to minus 95 ℃ and then comes out from the top, and is expanded to the pressure of 0.2MPa.a to 0.5MPa.a through the WMR hydraulic expansion machine 20 and then enters the WMR coiled pipe type heat exchanger 2 at the temperature of minus 70 ℃ to minus 100 ℃ to cool natural gas, WMR refrigerant and CMR refrigerant at the temperature of minus 65 ℃ to minus 95 ℃; the low pressure WMR (0.2 MPa.a-0.5 MPa.a, -35 ℃ to-45 ℃) from the bottom of the WMR coiled pipe heat exchanger 2 returns to the inlet buffer tank 17 of the WMR compressor for circulation.
3) The CMR refrigeration system provides cooling capacity for the complete liquefaction and supercooling of natural gas and CMR refrigerant:
the CMR refrigerant as the refrigerant of the CMR refrigeration system is pressurized to 5 MPa.a-8 MPa.a by a CMR compressor 22, then is cooled to 20-50 ℃ by an outlet cooler 23 of the CMR compressor, is cooled to-30-39 ℃ by a propane precooling plate-fin heat exchanger 1, is cooled to-65-95 ℃ by a WMR wound tube heat exchanger 2, is cooled to-155-160 ℃ in the CMR wound tube heat exchanger 3, then is discharged from the top, is expanded to 0.2-0.5 MPa.a by a CMR hydraulic expander 24, and then enters the CMR wound tube heat exchanger 3 to provide cold for natural gas and self-liquefaction supercooling; and the low-pressure CMR (0.2 MPa.a-0.5 MPa.a, -75 ℃ to-95 ℃) from the bottom of the CMR coiled heat exchanger 3 returns to the inlet buffer tank 21 of the CMR compressor for circulation.
4) High pressure LNG expansion flash
The natural gas from the top of the CMR coiled tube heat exchanger 3 is liquefied and subcooled to-155 to-160 ℃, the subcooled natural gas is expanded to (120kPa. a, -160 to-163 ℃) through an LNG hydraulic turbine expander 4 and then enters an LNG flash tank 5 for flash evaporation, BOG discharged by flash evaporation is sent to a downstream BOG supercharging device, and LNG at the bottom of the LNG flash tank 5 is supercharged through an LNG supercharging pump 6 and then sent to an LNG storage unit.
The mixed refrigerant WMR mainly comprises ethane and a certain amount of methane and propane, wherein the volume content of the methane is 5-15%, the volume content of the ethane is 70-85%, and the volume content of the propane is 10-20%; the CMR comprises nitrogen, methane and ethane, wherein the volume content of the nitrogen is 10-25%, the volume content of the ethane is 40-65%, and the volume content of the propane is 30-45%.
The utility model discloses a theory of operation is:
the utility model provides a three circulation liquefaction system based on high-efficient equipment can be applicable to the single-row annual capacity and reach 600 ~ 800 ten thousand tons/year super large-scale natural gas liquefaction device, and it adopts tertiary refrigeration cycle, and the precooling section adopts propane cryogen, liquefaction and mixed cryogen of supercooling section adoption; the pre-cooling cycle, the liquefaction cycle and the supercooling cycle respectively adopt a set of compression, cooling, condensation, turbine expansion and heat exchange processes.
In the utility model, the WMR, CMR and LNG throttle expansion adopt hydraulic turbine expansion machines, the principle of the hydraulic turbine expansion machines is isentropic expansion, and the refrigeration efficiency is higher; and the hydraulic turbine expander is adopted to recover energy for power generation, so that the comprehensive energy consumption is reduced.
The utility model discloses has following effect: 1) the composition and the proportion of the mixed refrigerant can be reasonably configured according to the environment of a project construction site and the change of the condition of the raw material gas, so that the cooling and liquefying temperature is optimized, the energy consumption of the whole process system is lowest, and the regional adaptability is wide; 2) and the three-stage refrigeration cycle adopts high-efficiency plate-fin heat exchangers and wound tube heat exchangers, has high heat exchange efficiency, can reasonably share refrigeration loads at all stages, and realizes the maximization of a single-line LNG device. 3) The WMR refrigerant and the CMR refrigerant are throttled by adopting a hydraulic turbine expander, so that the refrigeration efficiency is high, and the energy consumption of unit LNG products is lower; 4) the high-pressure LNG throttling adopts a hydraulic turbine expander, the throttling effect is good, and the natural gas liquefaction rate is higher.
Claims (6)
1. The utility model provides a three circulation natural gas liquefaction devices suitable for super large-scale which characterized in that: the system comprises a natural gas liquefaction pipeline, a propane precooling circulating system, a WMR refrigerating circulating system and a CMR refrigerating circulating system, wherein:
the natural gas liquefaction pipeline is formed by sequentially connecting a propane heat exchanger, a WMR heat exchanger, a CMR heat exchanger, an LNG expander, an LNG flash tank and an LNG booster pump;
the propane precooling circulating system comprises a propane heat exchanger, a propane compressor outlet cooler, a high-pressure propane gas-liquid separation tank, a medium-pressure propane gas-liquid separation tank and a low-pressure propane gas-liquid separation tank, and is used for precooling natural gas, WMR refrigerant and CMR refrigerant;
the WMR refrigeration cycle system comprises a WMR heat exchanger, a WMR compressor inlet buffer tank, a WMR compressor outlet cooler and a WMR expander and is used for further cooling and partially liquefying natural gas and CMR refrigerant;
the CMR refrigeration cycle system comprises a CMR heat exchanger, a CMR compressor inlet buffer tank, a CMR compressor outlet cooler and a CMR expander and is used for providing refrigeration capacity for the complete liquefaction and supercooling of natural gas and CMR refrigerant.
2. A three cycle natural gas liquefaction plant adapted for ultra-large scale use according to claim 1 and wherein: in the propane precooling circulating system, a propane compressor outlet cooler, a first high-pressure propane throttle valve, a propane heat exchanger and a propane compressor high-pressure suction inlet are sequentially connected; the propane compressor outlet cooler, the second high-pressure propane throttle valve, the high-pressure propane gas-liquid separation tank, the first medium-pressure propane throttle valve, the propane heat exchanger and the propane compressor medium-pressure suction inlet are sequentially connected; the high-pressure propane gas-liquid separation tank, the second medium-pressure propane throttle valve, the medium-pressure propane gas-liquid separation tank, the low-pressure propane throttle valve, the propane heat exchanger, the low-pressure propane gas-liquid separation tank and a low-pressure suction inlet of the propane compressor are sequentially connected; the gas phase at the outlet of the high-pressure propane gas-liquid separation tank is connected with a high-pressure suction pipeline of a propane compressor; the gas phase outlet of the medium-pressure propane gas-liquid separation tank is connected with a medium-pressure suction pipeline of a propane compressor.
3. A three cycle natural gas liquefaction plant adapted for ultra-large scale use according to claim 1 and wherein: in the WMR refrigeration cycle system, a WMR heat exchanger, a WMR compressor inlet buffer tank, a WMR compressor outlet cooler, a propane heat exchanger, a WMR expander and a WMR heat exchanger are connected in sequence.
4. A three cycle natural gas liquefaction plant adapted for ultra-large scale use according to claim 1 and wherein: in the CMR refrigeration cycle system, a CMR heat exchanger, a CMR compressor inlet buffer tank, a CMR compressor outlet cooler, a propane heat exchanger, a WMR heat exchanger, a CMR expander and a CMR heat exchanger are connected in sequence.
5. A three cycle natural gas liquefaction plant adapted for ultra-large scale use according to any of claims 1 to 4 and characterized by: the LNG expander, the WMR expander and the CMR expander are all hydraulic turbine expanders.
6. A three cycle natural gas liquefaction plant adapted for ultra-large scale use according to claim 5 and wherein: the propane heat exchanger is a plate-fin heat exchanger, and the WMR heat exchanger and the CMR heat exchanger are both wound tube heat exchangers.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110186251A (en) * | 2019-06-11 | 2019-08-30 | 中国石油工程建设有限公司 | It is a kind of to recycle natural gas liquefaction devices and method suitable for ultra-large three |
| CN114963689A (en) * | 2022-06-22 | 2022-08-30 | 中海石油气电集团有限责任公司 | Dual-cycle mixed refrigerant natural gas liquefaction system |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110186251A (en) * | 2019-06-11 | 2019-08-30 | 中国石油工程建设有限公司 | It is a kind of to recycle natural gas liquefaction devices and method suitable for ultra-large three |
| CN110186251B (en) * | 2019-06-11 | 2024-01-26 | 中国石油集团工程股份有限公司 | Three-cycle natural gas liquefaction device and method suitable for ultra-large scale |
| CN114963689A (en) * | 2022-06-22 | 2022-08-30 | 中海石油气电集团有限责任公司 | Dual-cycle mixed refrigerant natural gas liquefaction system |
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Effective date of registration: 20210304 Address after: No.2 Daqing East Road, Dushanzi District, Karamay City, Xinjiang Uygur Autonomous Region 834000 Patentee after: CNPC Engineering Co.,Ltd. Patentee after: CHINA PETROLEUM ENGINEERING & CONSTRUCTION Corp. Patentee after: CHINA NATIONAL PETROLEUM Corp. Address before: 100120 Xicheng District six paw Kang in Beijing City Patentee before: CHINA NATIONAL PETROLEUM Corp. Patentee before: CHINA PETROLEUM ENGINEERING & CONSTRUCTION Corp. |